Classifications

• • C—CHEMISTRY; METALLURGY
  • C07—ORGANIC CHEMISTRY
  • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
  • C07C51/00—Preparation of carboxylic acids or their salts, halides or anhydrides
  • C07C51/347—Preparation of carboxylic acids or their salts, halides or anhydrides by reactions not involving formation of carboxyl groups
  • C07C51/377—Preparation of carboxylic acids or their salts, halides or anhydrides by reactions not involving formation of carboxyl groups by splitting-off hydrogen or functional groups; by hydrogenolysis of functional groups
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • B01J27/00—Catalysts comprising the elements or compounds of halogens, sulfur, selenium, tellurium, phosphorus or nitrogen; Catalysts comprising carbon compounds
  • B01J27/14—Phosphorus; Compounds thereof
  • B01J27/16—Phosphorus; Compounds thereof containing oxygen, i.e. acids, anhydrides and their derivates with N, S, B or halogens without carriers or on carriers based on C, Si, Al or Zr; also salts of Si, Al and Zr
  • B01J27/18—Phosphorus; Compounds thereof containing oxygen, i.e. acids, anhydrides and their derivates with N, S, B or halogens without carriers or on carriers based on C, Si, Al or Zr; also salts of Si, Al and Zr with metals other than Al or Zr
  • B01J27/1802—Salts or mixtures of anhydrides with compounds of other metals than V, Nb, Ta, Cr, Mo, W, Mn, Tc, Re, e.g. phosphates, thiophosphates
  • B01J27/1806—Salts or mixtures of anhydrides with compounds of other metals than V, Nb, Ta, Cr, Mo, W, Mn, Tc, Re, e.g. phosphates, thiophosphates with alkaline or alkaline earth metals
• • B01J35/023—
• • B01J35/026—
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • B01J35/00—Catalysts, in general, characterised by their form or physical properties
  • B01J35/40—Catalysts, in general, characterised by their form or physical properties characterised by dimensions, e.g. grain size
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • B01J35/00—Catalysts, in general, characterised by their form or physical properties
  • B01J35/50—Catalysts, in general, characterised by their form or physical properties characterised by their shape or configuration
• • C—CHEMISTRY; METALLURGY
  • C07—ORGANIC CHEMISTRY
  • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
  • C07C51/00—Preparation of carboxylic acids or their salts, halides or anhydrides
  • C07C51/42—Separation; Purification; Stabilisation; Use of additives
  • C07C51/43—Separation; Purification; Stabilisation; Use of additives by change of the physical state, e.g. crystallisation
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • B01J27/00—Catalysts comprising the elements or compounds of halogens, sulfur, selenium, tellurium, phosphorus or nitrogen; Catalysts comprising carbon compounds
  • B01J27/14—Phosphorus; Compounds thereof
  • B01J27/16—Phosphorus; Compounds thereof containing oxygen, i.e. acids, anhydrides and their derivates with N, S, B or halogens without carriers or on carriers based on C, Si, Al or Zr; also salts of Si, Al and Zr
  • B01J27/18—Phosphorus; Compounds thereof containing oxygen, i.e. acids, anhydrides and their derivates with N, S, B or halogens without carriers or on carriers based on C, Si, Al or Zr; also salts of Si, Al and Zr with metals other than Al or Zr

Definitions

• the present disclosure relates to a method for preparing acrylic acid, and more particularly, to a method for preparing acrylic acid by dehydrating a lactic acid molecule.
• Acrylic acid is an organic compound having both a carboxylic acid and an unsaturated double bond in a molecule, is very simple in its structure and can be polymerized while being converted into various materials, and thus is used in various industrial fields.
• acrylic acid is used as polyacrylic acid, dots, adhesives, paints, etc. required for the production of a superabsorbent polymer, or can be used as a raw material for preparing other types of acrylate-based monomers, or may be used as a raw material for polymerizing with various other monomers such as acrylamide, acrylonitrile, styrene, and alpha olefin.
• Such acrylic acid is generally prepared using propylene produced in the process of refining and separating a crude oil, such as naphtha cracking.
• a method for preparing acrylic acid comprising the steps of: a first step of supplying an aqueous lactic acid solution to a reactor using a carrier gas; a second step of vaporizing the aqueous lactic acid solution; a third step of bringing the vaporized lactic acid molecule into contact with a dehydration catalyst; and a fourth step of obtaining acrylic acid, wherein the temperatures of the second to fourth steps are each independently adjusted.
• the second step may be performed under a temperature condition of about 200° C. to about 290° C., preferably under a temperature condition of about 200° C. or more, or about 230° C. or more, or about 250° C. or more and about 290° C. or less, or about 270° C. or less, or about 260° C.
• the second step may be performed in the presence of quartz.
• the third step may be performed under a temperature condition of more than 350° C. and about 400° C. or less, preferably under a temperature condition of more 350° C., or about 355° C. or more, or about 360° C. or more, and about 400° C. or less, or about 390° C. or less, or about 380° C. or less.
• the dehydration catalyst may include at least one selected from the group consisting of a calcium phosphate-based catalyst, a sodium phosphate-based catalyst, and an aluminum phosphate-based catalyst.
• the aqueous lactic acid solution in the first step, may be supplied at a flow rate of about 0.01 to about 10/hour, or at a flow rate of about 0.1 to about 5/hour, or about 0.1 to about 1/hour, based on a supply weight of lactic acid relative to a weight of the catalyst.
• a concentration of the aqueous lactic acid solution in the first step may be about 10 to about 80 wt %.
• the first to fourth steps are performed using a reactor equipped with a single reaction tube and a heating unit;
• the single reaction tube comprises a supply unit to which an aqueous lactic acid solution is supplied, a vaporization unit that vaporizes the aqueous lactic acid solution, a catalyst unit that brings the vaporized lactic acid molecule into contact with a dehydration catalyst; and a discharge unit that discharges acrylic acid;
• the heating unit comprises a first heating unit that heats the vaporization unit in a shape wrapping the single reaction tube, a second heating unit that is discontinuous with the first heating unit and heats a boundary portion between the vaporization unit and the catalyst unit and a front end of the catalyst unit, and a third heating unit this is discontinuous with the second heating unit and heats the rear end of the catalyst unit, and the temperatures of the second to fourth steps are each independently adjusted by the heating unit.
• the first heating unit may be heated so that the inside of the vaporization unit of the single reaction tube is maintained at a temperature condition of about 200° C. to about 290° C.
• the second heating unit and the third heating unit may be heated so that the inside of the catalyst unit of the single reaction tube is maintained at a temperature condition of more than 350° C. and about 400° C. or less.
• a set temperature of the second heating unit may be higher than a set temperature of the third heating unit.
• a set temperature of the second heating unit may be about 15° C. to about 30° C. higher than a set temperature of the third heating unit.
• a layer or an element in case a layer or an element is mentioned to be formed “on” or “above” layers or elements, it means that the layer or element is directly formed on the layers or elements, or it means that other layers or elements may be additionally formed between the layers, on a subject, or on a substrate.
• a method for preparing acrylic acid comprising the steps of: a first step of supplying an aqueous lactic acid solution to a reactor using a carrier gas; a second step of vaporizing the aqueous lactic acid solution; a third step of bringing the vaporized lactic acid molecule into contact with a dehydration catalyst; and a fourth step of obtaining acrylic acid, wherein the temperatures of the second to fourth steps are each independently adjusted.
• the first to fourth steps are performed using a reactor equipped with a single reaction tube and a heating unit;
• the single reaction tube comprises a supply unit to which an aqueous lactic acid solution is supplied, a vaporization unit that vaporizes the aqueous lactic acid solution, a catalyst unit that brings the vaporized lactic acid molecule into contact with a dehydration catalyst; and a discharge unit that discharges acrylic acid;
• the heating unit comprises a first heating unit that heats the vaporization unit in a shape wrapping the single reaction tube, a second heating unit that is discontinuous with the first heating unit and heats a boundary portion between the vaporization unit and the catalyst unit and a front end of the catalyst unit, and a third heating unit this is discontinuous with the second heating unit and heats the rear end of the catalyst unit, and the temperatures of the second to fourth steps are each independently adjusted by the heating unit.
• the present inventors have found that in a series of reactions to obtain acrylic acid by subjecting vaporized lactic acid molecules to a dehydration reaction in the presence of a catalyst, when the temperature of each step is independently adjusted by subdividing the vaporization step and the dehydration step, the efficiency of the reaction can be increased while reducing the generation of by-products, and the yield of acrylic acid and the conversion rate of lactic acid can be dramatically improved, thereby completing the present disclosure.
• the dehydration reaction that proceeds for the vaporized lactic acid molecule in the presence of a catalyst can be represented by the following reaction mechanism.
• the dehydration reaction of the lactic acid molecule can be explained as follows.
• a hydroxyl group linked to a carbonyl alpha position of the lactic acid molecule is released by a catalyst, hydrogen linked to a carbonyl beta position is also removed by a catalyst to form an acrylic acid anion, and then the hydrogen of the catalyst is linked to a carboxylate anion of acrylic acid to form acrylic acid.
• the reactants in the first step i.e., lactic acid supplied as a feed
• the aqueous lactic acid solution may be supplied at a flow rate of about 0.01 to about 10/hour, or 0.1 to about 5/hour, or about 0.1 to about 1/hour, based on the supply weight of lactic acid relative to the weight of the catalyst.
• lactic acid supplied as a feed may be supplied by a carrier gas.
• a carrier gas used at this time, an inert gas that does not affect the vaporization reaction or the dehydration reaction, such as nitrogen or a group 18 gas, can be used.
• the flow rate of the carrier gas used for the reaction may be about 1 to about 1000 times, or about 10 to about 500 times, or about 20 to about 300 times the supply amount of the aqueous lactic acid solution.
• the second step that is, the vaporization reaction of lactic acid molecules, is performed under a temperature condition of about 200° C. to about 290° C., preferably under a temperature condition of about 200° C. or more, or about 230° C. or more, or about 250° C. or more and about 290° C. or less, or about 270° C. or less, or about 260° C.
• the second step may be performed in the presence of quartz.
• the quartz may be in the form of quartz wool with a large surface area, or quartz particle.
• the lactic acid molecule supplied to the supply unit may be adsorbed onto the surface of the quartz wool or the like in the vaporization unit inside the reactor according to the flow of the carrier gas, and in this state, it may receive supply of heat from the quartz wool or the like to be vaporized.
• the reactor used for this reaction may be provided with a single reaction tube and a heating unit, and the heating unit may be a shape wrapping the single reaction tube.
• the first heating unit for heating the vaporization unit may be heated so that the inside of the vaporization part of the single reaction tube is maintained at a temperature condition of about 200° C. to about 290° C.
• a temperature as a reaction condition of each reaction and a set temperature of the first to third heating units positioned at each site of the reactor may be different from each other.
• the set temperature of the first to third heating units may be preferably set higher than the temperature of the respective corresponding reaction conditions. This may be because external gas and reactants are continuously supplied into a reactor according to the flow of the carrier gas, particularly, the temperature of the reactants supplied to the supply unit is commonly lower than the temperature of the vaporization unit, and in the vaporization unit, the temperature is continuously lowered due to the vaporization of lactic acid and water.
• the temperature of the vaporization unit where the vaporization reaction proceeds is lower than the temperature of the catalyst unit where the dehydration reaction proceeds.
• the first heating unit may be preferably set to a target temperature of the vaporization unit, that is, about 15 to about 30° C. higher than the preferred temperature of the above-mentioned vaporization reaction.
• the gaseous reaction product containing the vaporized lactic acid single molecule continues to move to a catalyst unit where the catalyst exists according to the flow of the carrier gas, and can be charged into a dehydration reaction, that is, the third step.
• the third step is performed under a temperature condition of more than 350° C. and about 400° C. or less, preferably under a temperature condition of more than 350° C., or about 355° C. or more, or about 360° C. or more, and about 400° C. or less, or about 390° C. or less, or about 380° C. or less.
• step 3 When the temperature of the third step is too low, there may be a problem that the lactic acid conversion rate and the acrylic acid yield are greatly reduced, and when the temperature in step 3 is too high, i) an aldehyde formation reaction by decarboxylation or decarbonylation reaction, ii) a propanoic acid formation reaction by reduction of acrylic acid, iii) a pentanedione formation reaction by condensation, and the like are more promoted, which may cause a problem that by-products are increased.
• the temperature of the catalyst unit as the dehydration reaction condition and the set temperature of the second and third heating units positioned at each site of the reactor may be different from each other.
• the second heating unit may be in the shape wrapping, in the interior of the reactor, i) a boundary portion between the vaporization unit and the catalyst unit and ii) a portion corresponding thereto in a single reaction tube for heating the front end of the catalyst unit.
• the third heating unit may be in the shape wrapping iii) a portion corresponding thereto in a single reaction tube for heating the rear end of the catalyst unit.
• the second heating unit and the third heating unit may be heated so that the inside of the catalyst unit of the single reaction tube is maintained at a temperature of more than 350° C. and about 400° C. or less.
• the set temperature of the second heating unit is higher than the set temperature of the third heating unit, specifically, it may be preferable that the set temperature of the second heating unit is about 15° C. to about 30° C. higher than the set temperature of the third heating unit.
• the second and third heating units are set higher than the target temperature of the catalyst unit, that is, about 15° C. to about 30° C. higher than the above-mentioned preferable temperature for the dehydration reaction.
• the second heating unit may be set to a higher temperature than the third heating unit, and for example, it may be set to about 15° C. to about 30° C. higher temperature.
• the temperature of the vaporization unit, the boundary portion between the vaporization unit and the catalyst unit, the front end of the catalyst unit, and the rear end of the catalyst unit are set differently according to the needs of each reaction.
• a separate heating unit that is, a second heating unit, capable of supplying heat is positioned at the boundary portion between the vaporization unit and the catalyst unit, where the temperature condition changes rapidly, whereby the energy efficiency can be further increased and also the reaction efficiency can be improved.
• the dehydration catalyst may include at least one selected from the group consisting of a calcium phosphate-based catalyst, a sodium phosphate-based catalyst, and an aluminum phosphate-based catalyst, and other reaction conditions can be used without any particular limitation as long as they are those generally used in the art to which the present disclosure pertains, and are not contrary to the content defined herein.
• the dehydration catalyst may include CaSO 4 /Na 2 SO 4 ; Na 4 P 2 O 7 /CaSO 4 ; Na 4 P 2 O 7 /Ca 3 (PO 4 ) 2 ; NaH 2 PO 4 —NaHCO 3 /SiO 2 ; AlPO 4 —NH 3 ; Ca 3 (PO 4 ) 2 /CaSO 4 ; Ca 2 P 2 O 7 ; Ca 5 (PO 4 ) 3 (OH) and the like.
• acrylic acid can be prepared from lactic acid with a high conversion rate and yield, and also energy consumption can be further reduced as compared with a conventional method.
• a reaction cylinder made of quartz with an inner diameter of 7 ⁇ 8 inches and a length of 860 mm was prepared as a single reaction tube.
• a non-reactive glass tube and quartz wool were added so that quartz sand is not poured down in a region of about 150 mm to about 300 mm from the upper end of the single reaction tube, and quartz sand was filled therein to form a vaporization unit.
• a catalyst obtained by molding a calcium phosphate catalyst into a cylindrical pellet having a diameter of about 3 mm and a length of about 3 mm was used.
• a non-reactive glass tube and quartz wool were placed in a region of a length of about 300 mm from the lower end of the vaporized portion so that the catalyst was not poured down, and about 50 g of the catalyst was filled therein to form a catalyst unit.
• a first heating unit having a length of about 200 mm was provided in a shape surrounding the entire region corresponding to the vaporization unit of the single reaction tube, from a position of about 100 mm downward from the top of the single reaction tube.
• a second heating unit having a length of about 100 mm was provided in a shape surrounding a boundary portion between the vaporization unit and the catalyst unit of a single reaction tube, and a region corresponding to the front end of the catalyst unit, from the rear end of the first heating unit.
• a third heating unit having a length of about 200 mm was provided in a shape surrounding a region corresponding to the rear end of the catalyst unit of the single reaction tube from the rear end of the second heating unit.
• a fourth heating unit having a length of about 200 mm was provided in a shape surrounding a region corresponding to a discharge unit of the single reaction tube from the rear end of the second heating unit.
• thermocouple was provided at the front and rear ends of the catalyst unit of the single reaction tube so as to measure the internal temperature.
• Nitrogen was used as a carrier gas, the flow rate was about 80 ml/min, and an aqueous lactic acid solution having a concentration of about 40 wt % was set at a flow rate of about 0.4 ml/min, and supplied to the reactor.
• the density of the supplied aqueous lactic acid solution was about 1.08 g/ml, the supply rate of the aqueous lactic acid solution was about 10.37 g/hour based on the amount of lactic acid, and it was calculated to be about 0.21/hour for the reference weight (1 g) of the supplied catalyst (50 g).
• the product sample obtained from the discharge unit was collected, cooled to about 4° C. in a condenser, and collected in the liquid phase, and the amount of acrylic acid obtained was confirmed by HPLC.
• the set temperatures of the first to fourth heating units were made respectively different from each other, and the temperatures of the front and rear ends of the catalyst unit were measured while performing the vaporization reaction and the dehydration reaction.
• the method for preparing acrylic acid according to an embodiment of the present disclosure can prepare acrylic acid from lactic acid with a high conversion rate and a high yield.

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• 2021
  • 2021-11-05 JP JP2023524945A patent/JP2023547431A/ja active Pending
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